US3149934A - Cyclic adsorption process - Google Patents

Cyclic adsorption process Download PDF

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US3149934A
US3149934A US123798A US12379861A US3149934A US 3149934 A US3149934 A US 3149934A US 123798 A US123798 A US 123798A US 12379861 A US12379861 A US 12379861A US 3149934 A US3149934 A US 3149934A
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adsorption
zone
desorption
component
feed
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Homer Z Martin
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/16—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B01D2257/7022—Aliphatic hydrocarbons
    • B01D2257/7025—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/0473—Rapid pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/0476—Vacuum pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/261—Drying gases or vapours by adsorption
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/20—Capture or disposal of greenhouse gases of methane

Definitions

  • this invention is directed towards an improvement in the method for fractionating gaseous mixtures taught in US. Patent 2,944, 627, issued to Charles W. Skarstrom on July 12, 1960.
  • the aforementioned patent the disclosure of which is hereby incorporated herein, is concerned with an adsorption process wherein a so-called key component is separated from a gaseous mixture.
  • the adsorption is carried out at a relatively high pressure and is followed by a desorption step at relatively low pressure.
  • the adsorbent is prevented from coming to equilibrium with the key. component in the gaseous material.
  • .rapid cycles permit the processing of large quantities of material and, furthermore, result in an oscillating concentration gradient within the adsorbent bed.
  • This desorbate is conventionally vented to the atmosphere or to other disposition than that of the purified unadsorbed product. Such procedure results in the loss of a considerable amount of the unadsorbed component.
  • the prior process may often be deficient.
  • the desorbate has a higher concentration of the adsorbed material than the feed, it was diluted with large amounts of the unadsorbed reflux material.
  • the desorbate stream may be of varying composition. Since it is advantageous to have a "ice constant composition feed mixture, it is desirable to pass the secondary efiiuent into a surge tank prior to its recycle.
  • the surge tank serves to average out the recycled composition. It may be located either before or after the compressor.
  • Another advantageous technique which may be employed with or without the surge tank is that of venting to the atmosphere the secondary efiiuent which is obtained at the beginning of the desorption cycle.
  • This initial secondary efiiuent has a comparatively low amount of the nonadsorbed component and hence it need not be recompressed and recycled with the later portions of the secondary eflluent.
  • the determination of when to start to recycle the secondary efiiuent is dependent on well known engineering considerations such as, for example. the amount of nonadsorbed component appearing and the economic value of such material.
  • a two-component system consisting of components A and N, i.e., the adsorbed and nonadsorbed component
  • the adsorbed and nonadsorbed component will be referred to.
  • multicomponent systems may be processed in accordance with this invention and, furthermore, that the terms adsorbed and nonadsorbed are used in a relative sense and should be more correctly referred to as the more readily adsorbed and the less readily adsorbed components.
  • the apparatus illustrated consists of two zones, X and Y, which contain an adsorbent advantageous for the desired separation.
  • the valves indicated by the letters x are opened when zone X is undergoing adsorption and zone Y desorption, while the valves lettered y are closed.
  • valves lettered y are opened and the valves lettered x are closed.
  • feed is introduced at a relatively high pressure through line 12 and passes through line 4x into adsorption zone X at a point intermediate to the ends thereof.
  • the feed Prior to introduction of the feed into the adsorption zone, the feed may be passed into a guard chamber (not shown). This chamber may serve to remove materials which will interfere with the main adsorption process.
  • the A component is adsorbed and a stream consisting essentially of the N component passes through valve 5x. This stream is referred to as the primary efiiuent.
  • a pressure reducing means 7 a portion of the stream is reduced to a relatively low pressure and passed through valve 8x into adsorption zone Y undergoing desorption.
  • the pressure reducing means 7 may be, for example, a valve or an orifice.
  • a portion of the primary effluent is recovered, while another portion as mentioned is used for the desorption.
  • half the total volume of primary effluent may be recovered, while the other half, after expansion in means 7, used for desorption.
  • Desorption zone Y maintained at a relatively low pressure, has a relatively high concentration of component A at the beginning of the desorption cycle. As desorption continues, the concentration of the A component is reduced and a stream containing both A and N is recovered through line 13.
  • this stream is passed through valve 9x and at least a part thereof is passed to compressor 3, wherein its pressure is increased from the relatively low pressure of zone Y to the relatively high pressure of zone X. A portion of this material, if desirable,
  • valve 14 may be vented to the atmosphere or recovered through line by making appropriate adjustment of valve 14.
  • the compressed material, richer in component A than the feed stream, is passed to a surge tank 17.
  • the surge tank serves to average out the desorbate composition.
  • a portion of compressed desorbate in surge tank 17 is recycled through valve 11x to the bottom of the adsorption zone X, wherein the A component is again adsorbed.
  • the introduction of feed is determined in such a manner that it enters the adsorption zone at a point wherein the time average concentration gradient is approximately the same as the feed.
  • the valves in the apparatus Prior to saturation of adsorption zone X, the valves in the apparatus are adjusted so as to discontinue the adsorption in zone X and to commence adsorption in zone Y. This is accomplished by opening the y valves and closing the x valves by any appropriate means such as by the use of a cycle timer connected to activate solenoids which open and close the valves.
  • various heat exchangers in difierent parts of the process may be incorporated to give the process a higher overall efficiency. Specifically, by heat exchanging the stream from the compression of the secondary efiiuent with the expanded portion of the primary efiluent, energy may be more effectively utilized. This exchange would serve to increase the heat in the reflux stream, thereby aiding desorption, and cool the compressed secondary efiiuent, thereby increasing the effectiveness of the subsequent adsorption.
  • the particular types of heat exchangers are well known to those skilled in the art.
  • the energy of expansion of the primary effiuent may be used to perform mechanical work, as for example, running the compressor.
  • FIGURE 2 shows a modification of the instant invention wherein two zones are connected in series, both for adsorption and desorption.
  • the feed is introduced at a point between the two adsorption zones.
  • the x valves are closed.
  • the reverse situation occurs when the Y zones are on adsorption and the X zones on desorption.
  • feed is introduced through line 20 and passes through valves 21x and line 22 into the upper adsorption zone X1.
  • the feed is introduced at a relatively high pressure.
  • valve 43 is closed since no material is passing through zone X2.
  • a stream containing a high concentration of the N component leaves zone X1 through line 23, passes through valve 24x and line 25.
  • This stream is referred to as the primary eflluent or adsorbate.
  • a predetermined portion of the material is removed from the process through valve 26.
  • At least a portion of the effluent from tower X1 is reduced in pressure as it passes through valve 27 and valve 28x and line 29, and passed into the top of zone Y1.
  • the desorption takes place at a relatively low pressure. It is presupposed herein that zones Y1 and Y2 had been saturated with the A component from a previous adsorption step.
  • the material free of the A component to a relatively low pressure serves to reduce the partial pressure of A, the adsorbed component, in zone Y1. Similarly, this material exits from zone Y1 through line 30, passes through valve 31 into zone Y2, wherein the latter zone is also desorbed. While for simplicity of operation it might be desirable to maintain zones Y1 and Y2 at the same pressure, it is also within the scope of this invention to use different relatively low pressures in the two zones. For example, it might be desirable to further reduce the pressure in zone Y2 since the purging material is no longer completely free from the adsorbed component.
  • a secondary effluent is withdrawn through line 32 and passes through valve 33x. A portion may be removed through valve 35x and 35 at this point in the process.
  • the secondary effluent is passed to compressor 37 via line 36.
  • Compressor 37 increases the pressure of the secondary eflluent from the relatively low desorption pressure to the relatively high adsorption pressure.
  • the secondary eflluent at line 38 may again be segregated if desirable and a portion removed from the process through valve 39 and line 40.
  • This compressed stream contains a higher partial pressure of A than exists in the feed.
  • At least a portion of the high pressure material is recycled via line 4-1 and valve 42x into the lower portion of adsorption zone X2. In this zone, the A component is adsorbed along the concentration gradient and a stream containing a concentration of components substantially the same as or greater than the primary feed is withdrawn through line 44.
  • valve 43 is open and the material flows through line 22 into the lower portion of the adsorption zone X1.
  • valve 4-3 remains open and the lower portion of zone X1 is continuously fed with material from line 44 and fed during the adsorption process.
  • zones X1 and X2 are maintained at the same relatively high pressure, it is within the scope of this invention that the pressures in these zones be unequal.
  • the partial pressure of A in the gas in contact with the solid is equal to or less than that corresponding to equilibrium with the adsorbed phase. This latter is limited to the partial pressure in the gas phase in contact with the adsorbent during the adsorptive opera tion.
  • the greatest partial pressure of A in the desorption gas equals that in the feed.
  • the concentration (expressed for example as mole fractions) of A in the desorption gas is greater than that in the feed gas.
  • the concentration of A on the adsorption solids at the bottom of the adsorber is increased and, as a result, the concentration of A in the desorber gas is clearly greater in the efiluent when the present invention is practiced than in the prior art systems, which had no recycle system as herein described.
  • this invention results in increased recovery of A and higher concentrations of A and N in overhead and desorbed streams, respectively.
  • the use of the instant invention is desirable in many types of separations, for example, in the recovery of hydrogen from hydrocarbon components, such as is common in many refinery streams, specifically Powerformer tail gas.
  • the process is invaluable in drying hydrogen and various other gases.
  • the recovery of C or C and C s from natural gas is a contemplated process.
  • a guard chamber for the removal of the higher molecular weight hydrocarbons. If these latter hydrocarbons (Cg-F) enter the adsorption zone, they rapidly contaminate the bed, lowering its capacity for the lower molecular weight hydrocarbons, e.g., methane.
  • the problem of desorbing these highly tenacious heavy hydrocarbons from the adsorbent has been partially solved by desorbing the adsorption zone under vacuum.
  • a guard chamber is employed, the heavy hydrocarbons are prevented from entering the adsorption zone, and therefore the latter zone need not be subject to vacuum desorption.
  • the heavy hydrocarbons may be removed from the guard chamber by vacuum desorption; but, since this chamber is considerably smaller than the adsorption zone, much smaller vacuum facilities are required.
  • the guard chamber may be independently treated in other manners, for example, it may be desirable to steam the guard chamber only or to treat the guard in a different time cycle from that of the main adsorptive bed.
  • the guard chamber could contain diflerent adsorbent material.
  • the feed material may be allowed to pass therethrough at a different velocity.
  • the guard can be in a separate vessel from the main adsorbent or so arranged that the depressuring gas from the main vessel bypasses the guard while permitting the purge gas to go through, that is, the guard chamber is depressured separately so that it is possible to have a higher velocity during the 'onstream time than in the main adsorber.
  • a typical guard bed is shown in feed line 12 as item 45 of FIGURE 1.
  • Line 46 can be used to clean up the guard bed by connecting it to .a source of vacuum or it can be used as an exit line if purge with an inert gas or part of the depressure gas is used.
  • void gas is meant that gas which accumulates in the voids between the adsorbent particles during adsorption.
  • This void gas which has approximately the same composition as the feed, is leaner in the adsorbed components than the desorbate.
  • adsorbents which should be used are well known to those skilled in the art. For example, if it is desirable to separate hydrogen from light hydrocarbons, activated char would be used. n the other hand, in drying processes, silica gel would be advantageous. It is well known in the art which adsorbents function preferably in particular separations, and such teachings could be readily incorporated along with the inventive features herein disclosed.
  • the various conditions maintained in the operation may also readily be selected by one skilled in the art. For example, the amount of reflux desired and the temperatures and relative pressures of the operation are discussed at length in US. Patent 2,944,627.
  • Example 1 Using the equipment described in FIGURE 1, a calculated process can be described as follows. A 50/50 hydrogen-methane mixture is subjected to adsorption at 500 p.s.i.a. at 70 F. The desorption may be carried out at p.s.i.a. and essentially the same temperature. The adsorbent employed may be about 560 pounds of activated charcoal in each adsorber. The adsorption-desorption time is about three minutes on each step. The feed rate is about 15,000 s.c.f.h. According to calculation, an essentially pure hydrogen secondary eflluent is recovered. When the reflux to feed ratio is 0.5, the hydrogen loss was only 25%. Comparative calculations show that where no reflux is employed a 50% hydrogen loss occurred. This clearly shows 'the improved recovery obtained by using the recycling technique of the instant invention.
  • While the instant invention is preferably directed towards an improvement in the process and apparatus taught in US. Patent No. 2,944,627, it need not be so limited.
  • rapid cycling is employed which results in the discontinuance of adsorption prior to saturation of the adsorbent.
  • the rapid cycling limits the delta T and thereby prevents the loss of heat by flow through the adsorption bed walls.
  • the improvement of the instant invention would be effective even if the above limitations on adsorption and cycle time were not adhered to. If for certain technical reasons it is found desirable to conduct adsorption until saturation, or to lengthen the cycle time, the inventive concept could still be employed.
  • the improvement which comprises: compressing at least a portion of the secondary effluent from said desorption zone, recycling said compressed secondary eflluent to the bottom of said adsorption zone, and introducing feed into the adsorption zone at a point intermediate the ends of the adsorption zone and wherein said primary eflluent contains substantially nonadsorbable components and said secondary efiluent contains a high concentration of adsorbable components relative to said feed.
  • a method for separating a gaseous feed containing components A and N which comprises: (1) simultaneously introducing said feed and a secondary effluent hereinafter specified into an adsorption zone containing an adsorbent selective of said A component, said feed being introduced at an intermediate point and said secondary eflluent being introduced at the bottom of said adsorption zone; (2) selectively adsorbing said A component; (3) withdrawing a primary eflluent from said zone containing substantially component N; (4) desorbing said A component by maintaining said adsorption zone at a relatively low pressure by introducing at least a portion of said primary efliuent; (5) withdrawing from said adsorption zone a secondary eflluent having a high concentration of A component relative to said feed; (6) compressing at least a portion of said secondary effluent; and (7) recycling at least a portion of said compressed secondary eflluent to the bottom of said adsorption zone as previously described.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2218799A1 (de) * 1971-04-20 1972-11-02 Petrocarbon Developments Ltd., Manchester (Großbritannien) Verfahren und Vorrichtung zum Trennen von Gemischen, insbesondere Gasgemischen
US3922149A (en) * 1974-01-30 1975-11-25 Garrett Corp Oxygen air enrichment method
US3925053A (en) * 1973-05-14 1975-12-09 Swift Chemical Company Slow acting fertilizer
US4104039A (en) * 1975-10-22 1978-08-01 Kuri Chemical Engineers, Incorporated Process for concentrating or liquefying a specified component of a gaseous mixture
US4153428A (en) * 1977-08-30 1979-05-08 Union Carbide Corporation Prepurification of toluene dealkylation effluent gas
EP0008512A1 (en) * 1978-08-21 1980-03-05 Air Products And Chemicals, Inc. Separation of multicomponent gas mixtures
EP0008882A1 (en) * 1978-08-21 1980-03-19 Air Products And Chemicals, Inc. Separation of multicomponent gas mixtures by pressure swing adsorption
US4349357A (en) * 1980-06-23 1982-09-14 Stanley Aviation Corporation Apparatus and method for fractionating air and other gaseous mixtures
US4354859A (en) * 1981-08-06 1982-10-19 Union Carbide Corporation Enhanced gas separation by selective adsorption
US4376639A (en) * 1981-12-10 1983-03-15 Calgon Corporation Novel repressurization of pressure swing adsorption system
US4386945A (en) * 1982-02-01 1983-06-07 Litton Systems, Inc. Process and compound bed means for evolving a first component enriched gas
US4415340A (en) * 1979-08-09 1983-11-15 Bergwerksverband Gmbh Adsorptive separation of gases
US4448592A (en) * 1981-08-18 1984-05-15 Linde Ag Adsorptive method for the separation of a gas mixture
US4491459A (en) * 1983-05-04 1985-01-01 Pinkerton Charles J Portable oxygen enrichment and concentration system
EP0201235A2 (en) * 1985-05-02 1986-11-12 The BOC Group plc Separation of a gas mixture
US4681602A (en) * 1984-12-24 1987-07-21 The Boeing Company Integrated system for generating inert gas and breathing gas on aircraft
US4702903A (en) * 1983-10-03 1987-10-27 Keefer Bowie Method and apparatus for gas separation and synthesis
US4732578A (en) * 1985-12-09 1988-03-22 Linde Aktiengesellschaft Pressure swing adsorption process
US4801308A (en) * 1983-10-03 1989-01-31 Keefer Bowie Apparatus and process for pressure swing adsorption separation
US5104426A (en) * 1989-11-08 1992-04-14 Hitachi, Ltd. Method of and apparatus for separating gas mixture
US5395427A (en) * 1994-01-12 1995-03-07 Air Products And Chemicals, Inc. Two stage pressure swing adsorption process which utilizes an oxygen selective adsorbent to produce high purity oxygen from a feed air stream
US5779768A (en) * 1996-03-19 1998-07-14 Air Products And Chemicals, Inc. Recovery of volatile organic compounds from gas streams

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US2747681A (en) * 1951-09-05 1956-05-29 British Oxygen Co Ltd Regeneration of adsorbent units
US2823764A (en) * 1957-02-08 1958-02-18 Jefferson Lake Sulphur Co Cyclic adsorption processes for removal and/or recovery of condensable hydrocarbons from natural gas
US2944627A (en) * 1958-02-12 1960-07-12 Exxon Research Engineering Co Method and apparatus for fractionating gaseous mixtures by adsorption
US2988502A (en) * 1957-04-26 1961-06-13 Exxon Research Engineering Co High efficiency hydrocarbon separation process employing molecular sieve adsorbents
US3102013A (en) * 1960-08-02 1963-08-27 Exxon Research Engineering Co Heatless fractionation utilizing zones in series and parallel

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US2614657A (en) * 1951-06-19 1952-10-21 Standard Oil Dev Co Adsorption of gases with charcoals having different activities
US2747681A (en) * 1951-09-05 1956-05-29 British Oxygen Co Ltd Regeneration of adsorbent units
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